EP0661373A1 - Entfernung von Verunreinigungen aus Synthesegas - Google Patents

Entfernung von Verunreinigungen aus Synthesegas Download PDF

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Publication number
EP0661373A1
EP0661373A1 EP94203782A EP94203782A EP0661373A1 EP 0661373 A1 EP0661373 A1 EP 0661373A1 EP 94203782 A EP94203782 A EP 94203782A EP 94203782 A EP94203782 A EP 94203782A EP 0661373 A1 EP0661373 A1 EP 0661373A1
Authority
EP
European Patent Office
Prior art keywords
synthesis gas
ammonia
water
supplied
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP94203782A
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English (en)
French (fr)
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EP0661373B1 (de
Inventor
Eva Christina Heyman
Pieter Lammert Zuideveld
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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Publication date
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Priority to EP94203782A priority Critical patent/EP0661373B1/de
Publication of EP0661373A1 publication Critical patent/EP0661373A1/de
Application granted granted Critical
Publication of EP0661373B1 publication Critical patent/EP0661373B1/de
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/406—Ammonia
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water

Definitions

  • the present invention relates to a process of removing contaminants such as ammonia from synthesis gas obtained from partially oxidizing in a gasification reactor a carbonaceous feed comprising the steps of
  • the treated aqueous stream is substantially free from ammonia, and if required this treated aqueous stream can be further treated.
  • the invention provides a process of removing contaminants such as ammonia from synthesis gas obtained from partially oxidizing in a gasification reactor a carbonaceous feed comprising the steps of
  • step (c) produces a more concentrated ammonia-containing aqueous stream that is supplied to the gasification reactor.
  • supplying the aqueous stream obtained in step (c) to the gasification reactor provides a simple way of removing ammonia from this stream.
  • the synthesis gas will also contain hydrogen cyanide, and some hydrogen cyanide will be absorbed in the water used to scrub the synthesis gas in step (a).
  • the bulk of the hydrogen cyanide is removed catalytically from the partly treated gas obtained in step (a).
  • the partly treated synthesis gas is contacted in a reactor in the presence of water with a hydrolysis catalyst, wherein downstream of the reactor excess water is removed from the synthesis gas to obtain further treated synthesis gas, and wherein the removed water is supplied to the stripper column.
  • ammonia is a product of the hydrolysis of hydrogen cyanide, this removed water will contain absorbed ammonia.
  • a carbonaceous feed such as coal, hydrocarbon oil, petroleum coke or natural gas
  • a gasification reactor 2 the carbonaceous feed is partially oxidized with an oxidant supplied through a conduit 3 to obtain a synthesis gas including carbon monoxide and hydrogen.
  • the oxidant can be steam or a free oxygen-containing gas such as oxygen, air, or oxygen enriched air.
  • the formed synthesis gas is withdrawn through a conduit 4. It will be appreciated that the conditions in the gasification reactor are known to those skilled in the art and will therefore not be described here in more detail.
  • This synthesis gas is contaminated with solids and gaseous contaminants such as ammonia, hydrogen sulphide, hydrogen cyanide and carbonyl sulphide. These contaminants have to be removed.
  • the synthesis gas is first cooled in a cooler 7 to a temperature at which the solids can be removed. Cooled synthesis gas is passed through a conduit 9 to a unit 13 for dry removal of solids from the gas. The solids are discharged from the solids removal unit 13 through a conduit 14, and synthesis gas from which solids have been removed is withdrawn through a conduit 16.
  • This synthesis gas is scrubbed with water in a first scrubber 18, which water is supplied through a conduit 20.
  • the amount of water is so selected that the synthesis gas is cooled to a predetermined temperature.
  • the ammonia present in the synthesis gas is absorbed in the water so that a first ammonia-containing aqueous stream is obtained.
  • Partly treated synthesis gas is withdrawn from the first scrubber 18 through a conduit 24 for further treatment. This further treatment will be discussed later.
  • the first ammonia-containing aqueous stream is passed from the first scrubber 18 through a conduit 22 to a stripper column 25.
  • the ammonia-containing aqueous stream is stripped with steam supplied through a conduit 26. Stripping the ammonia-containing aqueous stream produces an ammonia-containing gaseous stream and a treated aqueous stream which treated aqueous stream is supplied to the scrubber 18 through the conduit 20.
  • the stripper column 25 is sometimes referred to as the sour water stripper.
  • the ammonia-containing gaseous stream is supplied through a conduit 30 to a second scrubber 35.
  • the ammonia-containing gaseous stream is scrubbed with water supplied through a conduit 37 to obtain a second ammonia-containing aqueous stream and a treated gaseous stream which is withdrawn from the second scrubber 35 through a conduit 38.
  • the amount of water is so selected that it is sufficient to remove the ammonia concentrated in an aqueous stream.
  • the second ammonia-containing aqueous stream is supplied through a conduit 40 to the gasification reactor 2.
  • the ammonia concentration in the aqueous stream supplied to the gasification reactor 2 is much higher.
  • the partly treated synthesis gas withdrawn from the first scrubber 18 is passed through the conduit 24 to a reactor 45.
  • a hydrolysis catalyst to hydrolyse carbonyl sulphide and hydrogen cyanide.
  • the conditions in the hydrolysis reactor are known to those skilled in the art and will therefore not be discussed here in more detail.
  • An example of a suitable hydrolysis catalyst is a titania-containing catalyst as described in UK patent specification No. 2 159 132.
  • the gas stream is withdrawn from the reactor 45 through a conduit 47.
  • a condensor 48 excess water is removed from the gas stream, and this water contains ammonia from hydrolysing hydrogen cyanide.
  • Further treated synthesis gas is passed from the condensor 48 through a conduit 50.
  • the removed water is passed through a conduit 51 to the stripper column 25 where ammonia is removed in the same way as it was removed from the first ammonia-containing aqueous stream from the first scrubber column 18.
  • Water is removed from the gas in a condensor 75, and part of the water is supplied through a conduit 76 to the stripper column 25 where ammonia is removed in the same way as it is removed from the first ammonia-containing aqueous stream from the first scrubber column 18.
  • the gas enriched in hydrogen sulphide is supplied through a conduit 79 to a Claus plant 80 where hydrogen sulphide is converted to elemental sulphur which is withdrawn through a conduit 82.
  • a Claus plant and its operation are known to those skilled in the art and will therefore not be discussed here in more detail.
  • the gas leaving the Claus plant 80 through a conduit 84 is subjected to a reduction treatment in a reactor 85 to reduce in the presence of a reducing gas, such as hydrogen, sulphur compounds other than hydrogen sulphide to obtain a gas containing hydrogen sulphide.
  • a reducing gas such as hydrogen, sulphur compounds other than hydrogen sulphide
  • a suitable catalyst is a cobalt-molybdenum catalyst.
  • the conditions in the reactor are known to those skilled in the art and will not be discussed here in detail.
  • the reduced gas withdrawn through a conduit 87 is cooled in a cooler 88 by contacting it directly with water supplied through a conduit 89. After contacting the water is supplied through a conduit 93 to the stripper column 25 where ammonia is removed in the same way as it is removed from the first ammonia-containing aqueous stream from the first scrubber column 18.
  • the gas After cooling the gas is supplied through a conduit 95 to an absorption column 96 in which the gas is contacted with a lean absorbent solution to obtain loaded absorbent solution supplied through a conduit 97 to remove hydrogen sulphide from the gas. After contacting loaded absorption solution is supplied through a conduit 98 to the regeneration column 67 for regeneration. After contacting gas is withdrawn from the absorption column 96 through a conduit 100.
  • the conditions in the absorption column are known to those skilled in the art and will not be discussed here in detail.
  • the treated gaseous stream obtained in the second scrubber 35 is passed through the conduit 38 to the inlet of the Claus plant 80 to remove any sulphur Components from this stream.
  • Fig. 2 showing a second embodiment of the present invention.
  • Further treated synthesis gas is passed from the condensor 48 through the conduit 50 to a contactor 110.
  • the further treated synthesis gas is contacted with an aqueous reactant solution to oxidize hydrogen sulphide to elemental sulphur to obtain purified synthesis gas and spent reactant solution.
  • the aqueous reactant solution is supplied to the contactor 110 through a conduit 111, the purified synthesis gas is withdrawn through a conduit 112 and spent reactant solution is withdrawn from the contactor 110 through a conduit 113.
  • the aqueous reactant solution suitably contains a complex of Fe(III) with a chelating agent in the form of an organic acid such as nitrilotriacetic acid.
  • a complex of Fe(III) with a chelating agent in the form of an organic acid such as nitrilotriacetic acid.
  • Spent reactant solution is regenerated in a regenerator 115 by stripping it with air supplied through a conduit 116. From the regenerator are withdrawn regenerated reactant solution through the conduit 111, a stream rich in elemental sulphur through a conduit 118, and spent air through a conduit 119.
  • the conditions to oxidize Fe(II) to Fe(III) are known to those skilled in the art and will not be discussed here in detail.
  • Regenerated reactant solution is supplied through the conduit 111 to the contactor 110.
  • aqueous stream is supplied to the third scrubber 120 through a conduit 121.
  • Treated spent air is withdrawn from the third scrubber 120 through a conduit 125, and the aqueous stream is withdrawn through a conduit 127.
  • the aqueous stream can be passed to the first scrubber 18 for scrubbing the synthesis gas. Alternatively the aqueous stream is passed through a conduit 128 to the stripper column 25.
  • the treated gaseous stream obtained in the second scrubber 35 is passed through the conduits 38 and 130 to the inlet of the contactor 110 to remove any sulphur components from this stream.
  • the treated gaseous stream contains carbonyl sulphide it is suitably passed through the conduits 38 and 135 to the reactor 45 containing the hydrolysis catalyst.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Industrial Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Hydrogen, Water And Hydrids (AREA)
EP94203782A 1993-12-30 1994-12-28 Entfernung von Verunreinigungen aus Synthesegas Expired - Lifetime EP0661373B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP94203782A EP0661373B1 (de) 1993-12-30 1994-12-28 Entfernung von Verunreinigungen aus Synthesegas

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP93203726 1993-12-30
EP93203726A EP0661372A1 (de) 1993-12-30 1993-12-30 Entfernung von Verunreinigungen aus Synthesegas
EP94203782A EP0661373B1 (de) 1993-12-30 1994-12-28 Entfernung von Verunreinigungen aus Synthesegas

Publications (2)

Publication Number Publication Date
EP0661373A1 true EP0661373A1 (de) 1995-07-05
EP0661373B1 EP0661373B1 (de) 1999-03-03

Family

ID=8214255

Family Applications (2)

Application Number Title Priority Date Filing Date
EP93203726A Withdrawn EP0661372A1 (de) 1993-12-30 1993-12-30 Entfernung von Verunreinigungen aus Synthesegas
EP94203782A Expired - Lifetime EP0661373B1 (de) 1993-12-30 1994-12-28 Entfernung von Verunreinigungen aus Synthesegas

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EP93203726A Withdrawn EP0661372A1 (de) 1993-12-30 1993-12-30 Entfernung von Verunreinigungen aus Synthesegas

Country Status (8)

Country Link
EP (2) EP0661372A1 (de)
JP (1) JPH07257903A (de)
KR (1) KR950016836A (de)
CN (1) CN1040766C (de)
CA (1) CA2139166A1 (de)
DE (1) DE69416804D1 (de)
ES (1) ES2130349T3 (de)
ZA (1) ZA9410341B (de)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005123285A1 (en) * 2004-06-17 2005-12-29 Sorain Cecchini Ambiente Sca S.P.A. Method and system for the recycling of municipal solid wastes, and exploitation of the wasted solid recovery fuel
WO2009016139A1 (en) * 2007-07-31 2009-02-05 Shell Internationale Research Maatschappij B.V. Process for producing purified gas from gas comprising h2s, co2 and hcn and/or cos
WO2010078256A1 (en) 2008-12-31 2010-07-08 Shell Oil Company Process for producing a methane-rich gas
WO2010078254A2 (en) 2008-12-31 2010-07-08 Shell Oil Company Adiabatic reactor and a process and a system for producing a methane-rich gas in such adiabatic reactor
WO2010078252A2 (en) 2008-12-30 2010-07-08 Shell Oil Company Method and system for supplying synthesis gas
EP2236457A1 (de) * 2009-03-30 2010-10-06 Shell Internationale Research Maatschappij B.V. Verfahren zur Herstellung eines gereinigten Synthesegases
WO2010112502A1 (en) * 2009-03-30 2010-10-07 Shell Internationale Research Maatschappij B.V. Process for producing a purified synthesis gas stream
US8461216B2 (en) 2009-08-03 2013-06-11 Shell Oil Company Process for the co-production of superheated steam and methane
DE102012017045A1 (de) * 2012-08-29 2014-05-15 Thyssenkrupp Uhde Gmbh Verfahren zur Wäsche von schwefelhaltigen Gasen mit einer im Kreislauf geführten ammoniakhaltigen Waschlösung
US8927610B2 (en) 2009-08-03 2015-01-06 Shell Oil Company Process for the production of methane
US10518210B2 (en) 2016-11-22 2019-12-31 Mitsubishi Heavy Industries Engineering, Ltd. Gas clean-up unit and gas purification method

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3615878B2 (ja) * 1996-09-20 2005-02-02 三菱重工業株式会社 ガス化複合発電設備
US5929126A (en) * 1998-01-30 1999-07-27 Exxon Research And Engineering Co. Gas conversion with rejuvenation ammonia removal
US5948378A (en) * 1998-01-30 1999-09-07 Exxon Research And Engineering Co. Removal of ammonia and cyanide from synthesis gas with water production
AU766885B2 (en) * 1999-03-05 2003-10-23 Exxonmobil Research And Engineering Company Gas conversion with rejuvenation ammonia removal
US7022742B2 (en) * 2004-04-08 2006-04-04 Syntroleum Corporation Process to control nitrogen-containing compounds in synthesis gas
CA2715893C (en) * 2008-02-18 2018-06-12 Fluor Technologies Corporation Regenerator configurations and methods with reduced steam demand
CN102209582A (zh) * 2008-11-07 2011-10-05 国际壳牌研究有限公司 处理废气物流的方法与装置
IT1397745B1 (it) * 2010-01-22 2013-01-24 Siirtec Nigi S P A Processo integrato di purificazione di acque reflue di raffineria, contenenti prevalentemente ammoniaca ed acido solfidrico, e di gas acidi contenenti prevalentemente acido solfidrico.
US9856141B2 (en) * 2016-01-07 2018-01-02 Fluor Technologies Corporation Method for avoiding expensive sour water stripper metallurgy in a gasification plant

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US3079238A (en) * 1961-02-27 1963-02-26 Stearns Roger Mfg Company Gas purification system
US4073862A (en) * 1973-08-24 1978-02-14 Dr. C. Otto & Comp. G.M.B.H. Process for removing ammonia, hydrogen sulfide and hydrocyanic acid from gases
GB2024244A (en) * 1978-06-26 1980-01-09 Texaco Development Corp Production of clean hcn-free synthesis gas
US5112586A (en) * 1990-10-18 1992-05-12 Shell Oil Company Process for purification of synthesis gas
EP0487158A1 (de) * 1990-11-19 1992-05-27 Shell Internationale Researchmaatschappij B.V. Entsorgung von gebrauchtem Katalysator

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DE2043190C3 (de) * 1969-09-09 1979-02-15 Benson, Field & Epes, Berwyn, Pa. (V.St.A.) Verfahren zur Abtrennung von sauren Gasen aus heißen wasserdampfhaltigen Gasgemischen
NL7402037A (de) * 1973-02-16 1974-08-20

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3079238A (en) * 1961-02-27 1963-02-26 Stearns Roger Mfg Company Gas purification system
US4073862A (en) * 1973-08-24 1978-02-14 Dr. C. Otto & Comp. G.M.B.H. Process for removing ammonia, hydrogen sulfide and hydrocyanic acid from gases
GB2024244A (en) * 1978-06-26 1980-01-09 Texaco Development Corp Production of clean hcn-free synthesis gas
US5112586A (en) * 1990-10-18 1992-05-12 Shell Oil Company Process for purification of synthesis gas
EP0487158A1 (de) * 1990-11-19 1992-05-27 Shell Internationale Researchmaatschappij B.V. Entsorgung von gebrauchtem Katalysator

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100914150B1 (ko) * 2004-06-17 2009-08-28 쏘레인 체찌니 암비엔테 에스시에이 에스.피.에이. 도시 고형 폐기물의 리사이클링 방법 및 시스템, 및 폐기고형물 회수 연료의 이용
WO2005123285A1 (en) * 2004-06-17 2005-12-29 Sorain Cecchini Ambiente Sca S.P.A. Method and system for the recycling of municipal solid wastes, and exploitation of the wasted solid recovery fuel
US7772453B2 (en) 2004-06-17 2010-08-10 Sorain Cecchini Ambiente Sca S.P.A. Method for the recycling of municipal solid wastes
AU2008281856B2 (en) * 2007-07-31 2011-06-30 Shell Internationale Research Maatschappij B.V. Process for producing purified gas from gas comprising H2S, CO2 and HCN and/or COS
WO2009016139A1 (en) * 2007-07-31 2009-02-05 Shell Internationale Research Maatschappij B.V. Process for producing purified gas from gas comprising h2s, co2 and hcn and/or cos
US8475570B2 (en) 2007-07-31 2013-07-02 Shell Oil Company Process for producing purified gas from gas comprising H2S, CO2 and HCN and/or COS
CN101801506B (zh) * 2007-07-31 2012-10-10 国际壳牌研究有限公司 由含h2s、co2及hcn和/或cos的气体生产纯化气体的方法
WO2010078252A2 (en) 2008-12-30 2010-07-08 Shell Oil Company Method and system for supplying synthesis gas
WO2010078254A2 (en) 2008-12-31 2010-07-08 Shell Oil Company Adiabatic reactor and a process and a system for producing a methane-rich gas in such adiabatic reactor
US8470059B2 (en) 2008-12-31 2013-06-25 Shell Oil Company Process for producing a methane-rich gas
WO2010078256A1 (en) 2008-12-31 2010-07-08 Shell Oil Company Process for producing a methane-rich gas
WO2010112502A1 (en) * 2009-03-30 2010-10-07 Shell Internationale Research Maatschappij B.V. Process for producing a purified synthesis gas stream
WO2010112517A1 (en) * 2009-03-30 2010-10-07 Shell Internationale Research Maatschappij B.V. Process for producing a purified synthesis gas stream
EP2236457A1 (de) * 2009-03-30 2010-10-06 Shell Internationale Research Maatschappij B.V. Verfahren zur Herstellung eines gereinigten Synthesegases
US8772361B2 (en) 2009-03-30 2014-07-08 Shell Oil Company Process for producing a purified synthesis gas stream
US8461216B2 (en) 2009-08-03 2013-06-11 Shell Oil Company Process for the co-production of superheated steam and methane
US8927610B2 (en) 2009-08-03 2015-01-06 Shell Oil Company Process for the production of methane
DE102012017045A1 (de) * 2012-08-29 2014-05-15 Thyssenkrupp Uhde Gmbh Verfahren zur Wäsche von schwefelhaltigen Gasen mit einer im Kreislauf geführten ammoniakhaltigen Waschlösung
EP2890474A2 (de) * 2012-08-29 2015-07-08 ThyssenKrupp Uhde GmbH Verfahren zur wäsche von schwefelhaltigen gasen mit einer im kreislauf geführten ammoniakhaltigen waschlösung
US10518210B2 (en) 2016-11-22 2019-12-31 Mitsubishi Heavy Industries Engineering, Ltd. Gas clean-up unit and gas purification method

Also Published As

Publication number Publication date
JPH07257903A (ja) 1995-10-09
CN1040766C (zh) 1998-11-18
ES2130349T3 (es) 1999-07-01
CN1108294A (zh) 1995-09-13
CA2139166A1 (en) 1995-07-01
EP0661373B1 (de) 1999-03-03
DE69416804D1 (de) 1999-04-08
KR950016836A (ko) 1995-07-20
ZA9410341B (en) 1995-09-01
EP0661372A1 (de) 1995-07-05

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